CN105264292B - Burner - Google Patents
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- CN105264292B CN105264292B CN201480032446.0A CN201480032446A CN105264292B CN 105264292 B CN105264292 B CN 105264292B CN 201480032446 A CN201480032446 A CN 201480032446A CN 105264292 B CN105264292 B CN 105264292B
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- Prior art keywords
- oxidant
- burner
- oxidant gas
- section
- pipe
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- 239000007800 oxidant agent Substances 0.000 claims abstract description 181
- 230000001590 oxidative effect Effects 0.000 claims abstract description 170
- 238000000034 method Methods 0.000 claims abstract description 110
- 230000008569 process Effects 0.000 claims abstract description 105
- 239000007789 gas Substances 0.000 claims description 202
- 230000003197 catalytic effect Effects 0.000 claims description 16
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 11
- 238000011144 upstream manufacturing Methods 0.000 claims description 9
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- 229910021529 ammonia Inorganic materials 0.000 claims description 5
- 230000003647 oxidation Effects 0.000 claims description 5
- 238000007254 oxidation reaction Methods 0.000 claims description 5
- 230000008859 change Effects 0.000 claims description 4
- 239000000126 substance Substances 0.000 claims description 4
- 238000002485 combustion reaction Methods 0.000 description 12
- 239000011449 brick Substances 0.000 description 9
- 239000000463 material Substances 0.000 description 9
- 239000003054 catalyst Substances 0.000 description 7
- 230000009467 reduction Effects 0.000 description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 239000000446 fuel Substances 0.000 description 3
- 230000003068 static effect Effects 0.000 description 3
- OAKJQQAXSVQMHS-UHFFFAOYSA-N Hydrazine Chemical compound NN OAKJQQAXSVQMHS-UHFFFAOYSA-N 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 239000010410 layer Substances 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000011229 interlayer Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000037361 pathway Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000002787 reinforcement Effects 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
- F23D14/20—Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone
- F23D14/22—Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone with separate air and gas feed ducts, e.g. with ducts running parallel or crossing each other
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
- F23D14/02—Premix gas burners, i.e. in which gaseous fuel is mixed with combustion air upstream of the combustion zone
- F23D14/04—Premix gas burners, i.e. in which gaseous fuel is mixed with combustion air upstream of the combustion zone induction type, e.g. Bunsen burner
- F23D14/08—Premix gas burners, i.e. in which gaseous fuel is mixed with combustion air upstream of the combustion zone induction type, e.g. Bunsen burner with axial outlets at the burner head
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
- F23D14/46—Details, e.g. noise reduction means
- F23D14/48—Nozzles
- F23D14/58—Nozzles characterised by the shape or arrangement of the outlet or outlets from the nozzle, e.g. of annular configuration
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D91/00—Burners specially adapted for specific applications, not otherwise provided for
- F23D91/02—Burners specially adapted for specific applications, not otherwise provided for for use in particular heating operations
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D99/00—Subject matter not provided for in other groups of this subclass
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1235—Hydrocarbons
- C01B2203/1241—Natural gas or methane
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23D—BURNERS
- F23D2900/00—Special features of, or arrangements for burners using fluid fuels or solid fuels suspended in a carrier gas
- F23D2900/14—Special features of gas burners
- F23D2900/14064—Burner heads of non circular shape
Abstract
The invention discloses with the burner for being distributed in the multiple oxidant gas pipes of burner section everywhere and the process gas in plug flow, it provides the uniform mixing of oxidant and process gas.
Description
Technical field
The present invention relates to a kind of burner for catalytic reactor, the particularly burner for secondary reformer.
Background technology
Burner for the burning of reactant is mainly used in needing the gas of the stable flame with high combustion intensity to fire
Expect the burning of industrial furnace and process heater.This burner includes being had for fuel supply by what oxidant supply port wrapped
Central tube burner tube.The mixing of the reinforcement of fuel and oxidant in combustion zone is by making oxidant be passed through combustion
Realized at burner in face of the cyclone of central tube.Therefore, give oxidant stream eddy flow to move, this provides the height of combustion product
Inside and outside recycling and high combustion intensity.
More specifically, the burner in ammonia equipment is included for the burner in secondary reformer, wherein from tubulose
The conversion of methane of converter introduces to come in secondary reformer for the process streams of reactor via by oxidant (that is, air)
Middle continuation, therefore add nitrogen and be used for downstream ammonia ring, and generation is increased in secondary reformer catalysis by the burning of oxygen content
The temperature of conversion process in agent bed.For this application, conventional burner is nozzle ring burner.The burning of nozzle style type
Device equipped with the specially designed nozzle in each air dispensing hole, and attempt to realize the mixing at burner nozzle,
Equal gas Temperature Distribution at the low metal temperature of burner, catalyst bed inlet, and protection refractory lining is from warm
Flame core.Process gas only a part is burnt in secondary reformer, and remainder further flow to catalyst bed and steam turns
Change reaction.
Catalyst bed in secondary reformer is covered with the refractory brick perforated, to keep catalyst in place.Two process transform
Very high temperature causes refractory brick slowly to lose material by evaporation in stove, and the material then passes through the catalyst bed in lower section
Middle to condense to deposit, wherein temperature declines due to the heat dissipation steam reforming reaction occurred here.Unwanted result is to urge
The pressure drop of agent bed increases, and this can finally cause equipment downtime to remove the material of deposition.
The design of burner is critically important for minimizing the problem of catalyst bed pressure drop increases by said mechanism.Process Gas
The temperature of body catalytic oxidation agent gas can partly be increased to more than 2500 DEG C, and it is important in process gas and oxidant
The point/of initial contact between gas or multiple downstreams have good mixing.It is desirable that all process gas and burned
For journey gas mixing into a kind of mixture, it has (minimum possibility) consistent temperature before whole air-flows reach fire brick layer.
The situation conveys the minimum possible material given from refractory brick to catalyst bed.By contrast, when the gas not being thoroughly mixed
When stream reaches brick, there will be the region at the temperature lower than consistent temperature and the region of the temperature higher than consistent temperature.Phase
Than in the situation of consistent temperature, there is the situation of non-uniform temperature to cause and lost from the higher material of brick, because conveying mechanism
Sharp accelerated by raising temperature, and therefore the material loss of the increase from thermal region exceeds well over the reduction from cold-zone domain
Material loses.
The reduction of the pressure drop on burner in both oxidant gas side and Process Gas side is typically beneficial.Work as pressure
When drop reduces, if it means that compression stage is the bottleneck of equipment, peak flow rate (PFR) can be increased.Some ammonia equipment are with maximum
Its oxidant gas compressor is operated, and the oxidant gas side pressure drop reduced means that more oxidant gas can be supplied to
Journey air-flow.Process air-flow can similarly increase to keep the ratios constant between nitrogen and hydrogen, and effect is to increase hydrazine yield.Such as
Fruit stream increase is valueless, then reduces pressure drop and in most cases will imply that the cost drop for being related to required compression energy reduction
It is low.
Disclosed in U.S. Patent No. 5496170 it is a kind of be used for small-scale and medium-scale application turbulent burner,
It has the combustion product interior recirculation substantially reduced towards burner face.Disclosed in the patent burner design pass through to
Burner provides the oxidant eddy flow in the overall flow direction concentrated with the axis along combustion zone and drawn simultaneously towards same axis
Lead process air-flow and result in the stable flame of the unfavorable interior recirculation with high combustion intensity and without hot combustion product.
Disclosed turbulent burner includes combustion tube and central oxidizer supply pipe that is concentric with combustion tube and being spaced apart, so as to define
Annular process gas passage between pipe, oxidant supply pipe and process gas passage have single arrival end and individually gone out
Mouth end.U-shaped oxidant and fuel gas injector are arranged to coaxial at burner face.Burner is further equipped with band in oxidant
The bluff body of the static swirler blades of extension in injector.Swirler blades it is mounted thereto trip end and downstream hold between
On bluff body, and extend to the surface of oxidant jet chamber.
US2002086257 discloses a kind of turbulent burner with burner tube, and it includes central oxidizer supply pipe
With outer concentric fuel supply pipe, oxidant supply pipe be provided with concentric cylindrical guiding body, its have static swirler blades and
Central concentric cylindrical perforate, the swirler blades for the inner surface for extending to oxidant supply pipe from the outer surface of guiding body exist
It is concentrically arranged at the bottom of oxidant supply pipe in the space between guiding body and inwall.
EP0685685 describes a kind of gas injection nozzles, and it includes drain chamber, and drain chamber has cylinder shape inner wall,
And with the circular gas discharge orifice at its port of export, with one heart wrap the outer wall of inwall, outer wall is along at chamber outlet end
Region at continuous bend path, and at discharge orifice with inwall link sharp edges, wherein curved pathway have spy
Fixed radius of curvature.
Although above-mentioned effort overcomes the described problem for being related to burner, it has been thought that the burner of prior art design exists
Mode of operation will be challenged in the case of especially having challenge.
The content of the invention
Therefore, it is a primary object of the present invention to obtain burner design, it overcomes above mentioned problem.
Therefore, the present invention is according to the burner of the embodiment of claim, and it includes advantages below.
The low pressure drop of oxidant gas, this passes through the low flow velocity in oxidant gas side；It will not be produced by oxidant gas
It is raw to turn to；Similar flow passage for all oxidant gas tributaries of the straight tube through equal length.
Low process gas pressure drop, while plug flow is effectively produced, have in an embodiment by compared to one perforated plate
There are two perforated plates of the wall leakage of reduction.
Both of the above, while realize the overall goal of the substantially uniform temperature with the fire brick layer through reactor.
The successful mixing of process gas and oxidant gas is realized by one of two lines.One approach is to spend
Take big energy to produce significant turbulent flow, thus oxidizer flow (passes through during short flow passage in process gas
Before refractory brick in the confined space) effectively it is mixed into process air-flow.The example of the approach is using static mixer, rotation
See in stream device, injector or the simple design for the region for significantly increasing flow velocity.
Another approach is less oxidizer flow being subdivided into many subflows, and by these in a manner of well distributing
The process flow area of being fed to is everywhere.Each sprout of oxidant gas is mixed into the process air-flow of surrounding.Oxidant
The amount of gas and process gas balances everywhere in whole cross section in the same manner, and which results in identical temperature everywhere.Realize
The required flow passage length that this subdivision oxidizer flow is thoroughly mixed in the process gas of surrounding is when branch flow amount increases
Become smaller.This is that needs contact and the reduction distance between the oxidant gas and process gas of burning/mixing is (perpendicular to stream
Dynamic direction) natural result.
The present invention fall into second class above, because we attempt to have unanimously at the level of refractory brick
Temperature, while minimum cost is paid in terms of pressure drop.
The present invention includes being connected to the straight oxidant gas pipe of the certain amount of the oxidant gas pipe of entrance.These oxygen
The effluent of oxidant gas pipe is distributed on section, with matching process gas plug flow.The oxidant gas pressure drop of very little is taken,
Because pipe is straight, and parallel to the pipe of entrance, and because the oxidiser gas velocity in pipe keeps at a fairly low.Each oxidant
Flue is equipped with oval or plane section the special nozzle for being formed as having in its opening.This is critically important to reduce downstream
Mixing length, because jet stream is more effectively mixed into process air-flow than Circular Jet.(they are non-rotating right for the orientation of nozzle
Claim) it is selected to match the process everywhere on section as described above with the shape of the oxidant gas of position grouping
The amount of air-flow.
The prerequisite of layout for designing oxidizer gas nozzles is to know the process air-flow on section, because this is needed
Will be to the partly amount of balance oxidant gas and process gas.Preferably plug flow state is produced on Process Gas side,
So that flow velocity is constant everywhere in section.Although this makes it easier to be laid out oxidizer gas nozzles (substantially oxidant gas pipe
Should then be only geometrically equally distributed), but the Peak Flow Rate on section is changed into minimum possibility.The situation is away from (maximum
Nargin) critical situations of the oxidant gas pipe nozzle nearby with the region (backflow) recycled.Sprayed close to oxidant gas
And start the recycling of the nozzle at burning or backflow can cause very high temperature near metallic nozzle, cause them to melt or no
Then fragmentation.
The process gas inlet of most of secondary reformers comes from side, and is produced downwards in the neck of secondary reformer
The particular device that the plug flow of trip flowing needs.The present invention substitutes the common solution with a perforated plate using two perforated plates
Scheme.This is used for the more preferable flow distribution for producing process gas, while compared to the common solution using a perforated plate
Spend less pressure drop.In addition, burner is arranged in refractory liner container, so the very little between perforated plate and refractory walls is empty
Gap is not actual, because the dimensional tolerance on refractory portion is very big.We must receive the larger space at wall, but it means that this
In leakage stream, this is unwanted, because this does not meet generation plug flow.The undesirable effect makes in two perforated plate series connection
Become less serious when used time is compared to using only a perforated plate, twice of the pressure drop of each perforated plate with arranged in series.
Notable technology for implementation process gas plug flow is with long oxidant gas pipe, and allows process gas
Flow between them in available space, while process gas is rectified into plug flow form.
The first aspect of the present invention is a kind of burner, and it is applied to catalytic reactor, but it can be additionally used in other chemistry
Reactor.Burner includes oxidant gas inlet ports.Oxidant can be air.More than one oxidant gas inlet ports can make
With, but preferably one to reduce cost and pressure drop.Oxidant gas inlet ports may include the pipe into catalytic reactor, in a reality
Apply in example, at the top of reactor body.Multiple oxidant gas pipes are connected to oxidant gas inlet ports at its upstream at end.
In one embodiment, pipe is connected to the downstream of single tube further below, and it includes oxidant gas inlet ports.Oxidant nozzle is positioned at each
On the downstream of individual pipe.Burner also includes process gas inlet.In one embodiment, process gas inlet may also include list
Individual pipe, it in one embodiment can be at the side at the top of reactor.Oxidant gas pipe is arranged in adjacent tubes
There is sufficient spacing, to ensure that process gas can mix it in the oxidant gas with oxidant nozzle downstream between downstream
It is preceding to flow between the tubes.The length of each oxidant gas pipe is at least five times of the internal diameter of pipe.
In an embodiment of the present invention, multiple oxidant nozzles have non-circular exit opening section.Compared to circle
Exit opening, non-circular exit opening improve the mixing of oxidant gas and process gas.In certain embodiments of the invention,
Oxidant nozzle has oval exit opening section.Non-circular openings can by from least two opposite sides suppress pipe outlet
It is open to realize plastic deformation to provide.
In an embodiment of the present invention, the air-flow in reactor on different non-flat line directions by orienting come spontaneous combustion
The outlet oxidation agent air-flow of device optimizes.In this way, oxidant gas and the process gas that is mixed with oxidant gas
Air-flow may be adapted to the shape and volume of the reactor in burner downstream.
For the mixing of further oxidation reinforced dose of gas and process gas, at least one (preferably two) perforated plate is located at
Between process gas inlet and oxidant jet expansion opening.This balances the section through burner towards the ideal situation of plug flow
Process air-flow.By with more than one perforated plate, the minimum pressure loss on this Process Gas side by burner
And therefore minimize also bypass process streams and realize, bypass process streams due to dimensional tolerance may alternatively appear in the external diameter of perforated plate with
Between the internal diameter of reactor wall.
In an embodiment of the present invention, be distributed in order to ensure the Uniform Flow of process gas, between two perforated plates away from
From at least a quarter of the diameter for perforated plate.In this way, compared to they cover area, for two perforated plates it
Between distance ensure that minimum length and area ratio.Perforated plate can not have identical diameter；In the case, two perforated plates it
Between distance should be minimum perforated plate diameter at least half, this is actually generally by for closest to process gas inlet
Perforated plate.
In another embodiment of the present invention, oxidant gas pipe is arranged to oxidant flow direction, itself and oxygen
The flow direction of oxidant gas entrance is into less than 45 °, preferably, the upstream end of oxidant gas pipe has oxidizer flow side
To it is with the oxidizer flow direction in oxidant gas inlet ports into less than 10 °.
In an embodiment of the present invention, by the oxidant gas pipe with 3 or more than 3, and in another implementation
In example, by ensuring the enough of the distribution for the process gas between oxidant gas pipe with band at least 20mm length
The oxidant gas pipe of downstream space, there is provided oxidant gas pipe (and the therefore oxidant and process in oxidant nozzle downstream
The height mixing of gas) between process air-flow be uniformly distributed.
The second aspect of the present invention is the method for the burn process gases in catalytic reactor.Two strands of air-flows provide to
The burner of installation in the reactor, for example, in the top of reaction.It is first-class including oxidant；This is provided to the oxygen of burner
Oxidant gas entrance；Second includes providing to the process gas of the process gas inlet of burner.It is first-class from oxidant gas
Body entrance flows through multiple oxidant gas pipes, and it is connected to oxidant gas inlet ports at its upstream at end, there is provided from oxidant
Gas access and the current path for passing through each pipe.Oxidant gas flows further through pipe until and passing the downstream for being arranged in pipe
Oxidant nozzle at end.Nozzle has non-circular outlet, and it gives oxidant gas " flat " section for leaving nozzle, and because
If this give section compared to the oxidant gas of outflow in the case of circular (this strengthens the mixing with process gas) more
High surface and area of section ratio.Nozzle can be the single unit for being connected to pipe, or they can be non-circular to be manufactured into
The end of pipe.Second air-flow further flows into burner from process gas inlet, and in this place, it is uniformly distributed to burner
Whole cross section.This is possible, because pipe is arranged to have enough spacing between them, and is specifically in adjacent pipe
Between downstream, to allow and ensure that the second between pipe flows.In burner downstream, when second is through burner
When distributing, second passes through the exit opening of nozzle, and the mixing of first-class and second sectional uniform.
In another embodiment of the second aspect of the present invention, second passes through at least two perforated plates, and it was located at
Between journey gas access and oxidant jet expansion opening.Therefore second is more effectively evenly distributed to burning in short distance
In the whole cross section of device, which save space and material cost.
In another aspect of the present invention, burner as described above is used to perform in chemical reactor to be catalyzed
Journey.The present invention this third aspect another more specifically in embodiment, chemical reactor is two sections in ammonia equipment and turned
Change stove.
Inventive features
1. for the burner of catalytic reactor, including oxidant gas inlet ports, process gas inlet, hold at its upstream
Place is connected to multiple oxidant gas pipes of oxidant gas inlet ports, and the oxidant nozzle of each pipe downstream end, wherein
Pipe is arranged to the abundant spacing for having between the downstream of adjacent tubes, to ensure process gas before being mixed with oxidant gas
Flow between the tubes, the length of each pipe is at least five times of the internal diameter of pipe.
2. according to the burner of feature 1, plurality of oxidant nozzle has non-circular exit opening section.
3. according to the burner of feature 2, wherein the non-circular exit opening section is ellipse.
4. according to the burner of feature 2, wherein the non-circular exit opening section of the oxidant nozzle is by from least two
Realized until realizing the plastic deformation of the pipe outlet of individual opposite side compacting pipe.
5. according to the burner of any one of preceding feature, wherein the orientation of each oxidant nozzle limits oxidant
Gas vent direction, and the export direction of wherein at least two oxidant nozzle is not parallel.
6. according to the burner of any one of preceding feature, wherein at least one perforated plate is located at process gas inlet
Between oxidant jet expansion opening, so as to balance the process air-flow through the section of burner.
7. according to the burner of feature 6, two of which perforated plate is located at process gas inlet and opened with oxidant jet expansion
Between mouthful, therefore towards plug flow balance through the process air-flow in the section of burner, but make the pressure loss as caused by perforated plate most
Smallization.
8. according to the burner of feature 7, the distance between two of which perforated plate is to be located nearest to process gas inlet
Perforated plate diameter at least a quarter.
9. according to the burner of any one of preceding feature, wherein oxidant gas pipe is arranged so that oxidant gas
The flow direction in flow direction and oxidant gas inlet ports in body pipe is into the angle less than 45 °.
10. according to the burner of any one of preceding feature, wherein the number of oxidant gas pipe be 3 or 3 with
On.
11. according to any one of feature 6-10 burner, wherein at least one perforated plate has in the perforated plate
Equally distributed perforation on area of section, so as to provide the pressure drop of the balance on the area of section.
12. according to any one of feature 6-10 burner, wherein at least one perforated plate has perforation, and it is suitable to root
According to the process air-flow and pressure distribution above the perforated plate, worn by the distribution of perforation or the change in size of perforation described
Equilibrium pressure drop is provided on the area of section of orifice plate.
13. according to any one of feature 6-12 burner, wherein at least one perforated plate has perforation, its be band extremely
Few 4mm, preferably at least 12mm diameter circular hole.
14. according to the burner of any one of preceding feature, the length of wherein oxidant gas pipe is at least 20mm.
15. a kind of method of the burn process gases in catalytic reactor, comprises the following steps：
First-class including oxidant is provided to the oxidant gas inlet ports of the burner in catalytic reactor,
Second including process gas is provided to the process gas inlet of burner,
First-class flow through from oxidant gas inlet ports is set to be connected to the more of oxidant gas inlet ports at end at its upstream
Individual oxidant gas pipe and the spray of the oxidant with non-circular exit opening section for flowing through the downstream end for being arranged in each pipe
Mouth,
The second from process gas inlet is set to flow between the tubes, pipe is arranged to have between the downstream of adjacent tubes
Enough spacing, to ensure that second can flow between the tubes,
First-class and second is mixed in the area of the outlet downstream of oxidant nozzle.
16. according to the method for being used for the burn process gases in catalytic reactor of feature 15, in addition to intermediate steps：
Second is set to flow through at least two perforated plates between process gas inlet and oxidant jet expansion opening, so as to balance
Through the flowing of the second in the section of burner.
17. it is used for the purposes that catalytic process is performed in chemical reactor according to the burner of any one of feature 14.
18. the purposes for the secondary reformer being used for according to any one of feature 1-14 burner in ammonia equipment.
Location label
01. burner.
02. catalytic reactor.
03. oxidant gas inlet ports.
04. process gas inlet.
05. oxidant gas pipe.
06. oxidant nozzle.
07. perforated plate.
Embodiment
Fig. 1 shows the side cross-sectional view of burner 01.It is arranged in the top of catalytic reactor 02, and reactor 02 is
Cylinder and top section have reduce diameter.
Oxidant gas enters burner via oxidant gas inlet ports 03, and the single tube at center is arranged on the most top of reactor
In portion.Through oxidant gas inlet ports, oxidant gas further flows downward via multiple oxidant gas pipes 05, and pipe 05 exists
The downstream for the central tube for forming oxidant gas inlet ports is connected at its upstream end.As visible on accompanying drawing, multiple oxidant gas
The flow direction of oxidant gas in each in body pipe and the stream of the oxidant gas in central oxidizer gas inlet pipe
Dynamic direction is substantially the same.This needs the low pressure drop in the oxidant gas side of burner.
The distance between adjacent tubes increase from the upstream end of oxidant gas pipe to downstream, so as to be passed through in oxidant gas
Flowed out by oxidant nozzle 06 and oxidant gas is uniformly distributed in the total cross-sectional area of burner and the point flowed into reactor
Body, oxidant nozzle 06 are located at each downstream end of multiple oxidant gas pipes.In addition, between adjacent oxidant gas pipe this
The spacing of sample increase allows and ensure that process gas flows between flue.
Process gas enters in burner via the process gas inlet 04 at the top side of catalytic reactor.Cross
Journey gas access includes single pipe, and it provides the process of the axis perpendicular to burner, oxidant gas inlet ports and reactor
Air-flow.Process gas exists before this contributes in the reactor that process gas enters burner and oxidant jet expansion downstream
The area of section of burner being uniformly distributed everywhere.For being uniformly distributed for further enhance process gas, two perforated plates 07
Between process gas inlet and oxidant jet expansion opening.Perforated plate provides pressure drop, and " braking interlayer ", it forces process
Gas distributes.Two perforated plates more effectively work than one, because providing the preferable distribution of the substantially plug flow of process gas
If can be with identical or than being realized using the lower overall presure drop of only one perforated plate.Further, since the external diameter of perforated plate with
Bypass reduces compared to single perforated plate caused by tolerance between inner top reactor wall.
When the process gas evenly distributed in two perforated plate downstreams eventually arrives at oxidant jet expansion, it is substantially
With plug flow.Oxidant nozzle has the oval exit opening section as that can be more clearly seen in Fig. 2, its for burner etc.
Away from view, and reactor or process gas inlet are not showed that.Oval exit opening section provides each oxidation in mixed zone
The larger surface of agent air-flow and area ratio, and thus provide and mixed with the more effective of process gas.
Example
Compared to the annular burner of original design, the research of concept proposed by the present invention is carried out using CFD.The base used
Plinth case (flow data) is derived from physical device.
Research shows that the pressure loss on the Process Gas side of the burner of the present invention is fired compared to conventional annular nozzle
Burner reduces by 22.3%.The pressure loss in the air side of the burner of the present invention reduces compared to conventional annular jet-burner
80.3%。
See that the new burner concept of the present invention provides the huge reduction of air wide pre. drop.
It is also clear that the new burner concept of the present invention is latent with material evaporation due to having reduced maximum temperature
Power.
We also have been realized in the reduction in gas side pressure drop.It is noted, however, that annular burner and the present invention it is new
The gas side pressure drop of both burner concepts all has at a fairly low absolute value.
Finally, from flowing viewpoint it may be said that we have obtained the notable preferably burning with the new burner concept of the present invention
Device.
Claims (16)
1. for the burner of catalytic reactor, it includes oxidant gas inlet ports, process gas inlet, multiple oxidant gas
The oxidant nozzle of pipe and each oxidant gas pipe downstream end, the multiple oxidant gas pipe is at its upstream at end
The oxidant gas inlet ports are connected to, wherein the multiple oxidant gas pipe is arranged to have adjacent oxidant gas pipe
Downstream between abundant spacing, to ensure process gas before being mixed with oxidant gas in the multiple oxidant gas
Being flowed between body pipe, the length of each oxidant gas pipe is at least five times of the internal diameter of oxidant gas pipe, and
Wherein, two perforated plates are located between the process gas inlet and the exit opening of the oxidant nozzle, so as to flat
The process air-flow to have weighed through the section of the burner towards plug flow so that as the pressure loss caused by these perforated plates most
Smallization.
2. burner according to claim 1, it is characterised in that there is multiple oxidant nozzles non-circular outlet to open
Mouth section.
3. burner according to claim 2, it is characterised in that the non-circular exit opening section is ellipse.
4. burner according to claim 2, it is characterised in that the non-circular exit opening section of the oxidant nozzle
By suppressing the outlet of the multiple oxidant gas pipe from least two opposite sides until realizing the multiple oxidant gas
The plastic deformation of pipe is realized.
5. according to the burner described in any one of preceding claims 1-4, it is characterised in that each oxidant nozzle is determined
To the export direction for defining the oxidant gas, and wherein, the export direction of at least two oxidant nozzles is not
It is parallel.
6. according to the burner described in any one of preceding claims 1-4, it is characterised in that at least one perforated plate is located at
Between the exit opening of the process gas inlet and the oxidant nozzle, so as to balance through the section of the burner
The process air-flow.
7. burner according to claim 1, it is characterised in that the distance between described two perforated plates are positioned at most connecing
At least a quarter of the diameter of the perforated plate of the nearly process gas inlet.
8. according to the burner described in any one of preceding claims 1-4, it is characterised in that the multiple oxidant gas
Pipe is arranged so that the flow direction in the multiple oxidant gas pipe and the flow direction in the oxidant gas inlet ports
Into the angle less than 45 °.
9. according to the burner described in any one of preceding claims 1-4, it is characterised in that the multiple oxidant gas
The number of pipe is 3 or more than 3.
10. burner according to claim 6, it is characterised in that at least one perforated plate has in the perforation
Equally distributed perforation on the area of section of plate, so as to provide the pressure drop of the balance on the area of section.
11. burner according to claim 7, it is characterised in that at least one perforated plate is located at the process gas and entered
Between mouth and the exit opening of the oxidant nozzle, so as to balance the process air-flow through the section of the burner,
At least one perforated plate has the equally distributed perforation on the area of section of the perforated plate, so as to provide the section
The pressure drop of balance on area.
12. burner according to claim 8, it is characterised in that at least one perforated plate is located at the process gas and entered
Between mouth and the exit opening of the oxidant nozzle, so as to balance the process air-flow through the section of the burner,
At least one perforated plate has the equally distributed perforation on the area of section of the perforated plate, so as to provide the section
The pressure drop of balance on area.
13. burner according to claim 9, it is characterised in that at least one perforated plate is located at the process gas and entered
Between mouth and the exit opening of the oxidant nozzle, so as to balance the process air-flow through the section of the burner,
At least one perforated plate has the equally distributed perforation on the area of section of the perforated plate, so as to provide the section
The pressure drop of balance on area.
14. a kind of method for being used for the burn process gases in catalytic reactor, comprises the following steps：
First-class including oxidant is provided to the oxidant gas inlet ports of the burner in the catalytic reactor,
Second including process gas is provided to the process gas inlet of the burner,
Make from the oxidant gas inlet ports it is described it is first-class flow through multiple oxidant gas pipes and flowing through be arranged in it is each
The oxidant nozzle with non-circular exit opening section of the downstream end of oxidant gas pipe, the multiple oxidant gas
Pipe is connected to the oxidant gas inlet ports at its upstream at end,
The second from the process gas inlet is set to be flowed between the multiple oxidant gas pipe, the multiple oxidation
Agent flue is arranged to have enough spacing between the downstream of adjacent oxidant gas pipe, to ensure that the second can
Flowed between the multiple oxidant gas pipe,
Described first-class and described second is mixed in the area of the outlet downstream of the oxidant nozzle, and
Wherein, methods described also includes intermediate steps：
Second is set to flow through at least two between the exit opening of the process gas inlet and the oxidant nozzle
Perforated plate, so as to balance the flowing of the second through the section of the burner so that by least two perforated plate
The caused pressure loss minimizes.
15. the burner according to any one of claim 1 to claim 13 is used to perform in chemical reactor to urge
The purposes of change process.
16. the secondary reformer that the burner according to any one of claim 1 to claim 13 is used in ammonia equipment
Purposes.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP13171027.9 | 2013-06-07 | ||
| EP13171027.9A EP2811228B1 (en) | 2013-06-07 | 2013-06-07 | Burner |
| PCT/EP2014/060811 WO2014195168A1 (en) | 2013-06-07 | 2014-05-26 | Burner |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105264292A CN105264292A (en) | 2016-01-20 |
| CN105264292B true CN105264292B (en) | 2018-01-19 |
Family
ID=48613447
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201480032446.0A Active CN105264292B (en) | 2013-06-07 | 2014-05-26 | Burner |
Country Status (14)
| Country | Link |
|---|---|
| US (1) | US10082289B2 (en) |
| EP (1) | EP2811228B1 (en) |
| CN (1) | CN105264292B (en) |
| BR (1) | BR112015030027B1 (en) |
| CA (1) | CA2910908C (en) |
| DK (1) | DK2811228T3 (en) |
| EA (1) | EA032737B1 (en) |
| ES (1) | ES2748179T3 (en) |
| IL (1) | IL242086B (en) |
| MX (1) | MX365759B (en) |
| MY (1) | MY173755A (en) |
| PL (1) | PL2811228T3 (en) |
| UA (1) | UA119040C2 (en) |
| WO (1) | WO2014195168A1 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BR112018012974B1 (en) * | 2015-12-23 | 2022-12-27 | Flsmidth A/S | BURNER FOR ONE OVEN AND ROTARY OVEN |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5562437A (en) * | 1993-06-22 | 1996-10-08 | Enterprise Generale De Chauffage Industriel Pillard (Societe Anonyme) | Liquid or gaseous fuel burner with very low emission of nitrogen oxides |
| DE19850940A1 (en) * | 1998-11-05 | 2000-05-31 | Messer Austria Gmbh Gumpoldski | Swirl burner |
| EP1783426A1 (en) * | 2005-11-07 | 2007-05-09 | Riello S.p.A. | Combustion head for a gas burner |
| CN101956974A (en) * | 2009-07-16 | 2011-01-26 | 毛羽 | Novel high-efficiency and low-NOx gas burner capable of controlling flame profile |
| CN202277828U (en) * | 2010-02-18 | 2012-06-20 | 赫多特普索化工设备公司 | Combustor |
Family Cites Families (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3901445A (en) | 1974-11-08 | 1975-08-26 | Pullman Inc | Gas burner - lance construction |
| DK168460B1 (en) | 1991-12-06 | 1994-03-28 | Topsoe Haldor As | Swirl burner |
| US5390857A (en) | 1994-06-01 | 1995-02-21 | Haldor Topsoe A/S | Gas injector nozzle |
| CA2361704C (en) | 1999-02-10 | 2009-12-15 | Casale Chemicals S.A. | Secondary reforming process and burner |
| US6174159B1 (en) | 1999-03-18 | 2001-01-16 | Precision Combustion, Inc. | Method and apparatus for a catalytic firebox reactor |
| US6358040B1 (en) * | 2000-03-17 | 2002-03-19 | Precision Combustion, Inc. | Method and apparatus for a fuel-rich catalytic reactor |
| DE60113792T2 (en) | 2001-01-04 | 2006-06-22 | Haldor Topsoe A/S | swirl burner |
| CN100341616C (en) | 2003-06-23 | 2007-10-10 | 卡萨尔化学股份有限公司 | Secondary reforming equipment |
| US20070089417A1 (en) * | 2005-10-06 | 2007-04-26 | Khanna Vivek K | Catalytic reformer with upstream and downstream supports, and method of assembling same |
| US20100104990A1 (en) * | 2008-10-23 | 2010-04-29 | Sarmiento-Darkin Wladimir Y | Wide flame burner |
| US8632621B2 (en) * | 2010-07-12 | 2014-01-21 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for melting a solid charge |
-
2013
- 2013-06-07 DK DK13171027T patent/DK2811228T3/en active
- 2013-06-07 EP EP13171027.9A patent/EP2811228B1/en active Active
- 2013-06-07 ES ES13171027T patent/ES2748179T3/en active Active
- 2013-06-07 PL PL13171027T patent/PL2811228T3/en unknown
-
2014
- 2014-05-26 MX MX2015015931A patent/MX365759B/en active IP Right Grant
- 2014-05-26 EA EA201600001A patent/EA032737B1/en not_active IP Right Cessation
- 2014-05-26 CA CA2910908A patent/CA2910908C/en active Active
- 2014-05-26 MY MYPI2015002866A patent/MY173755A/en unknown
- 2014-05-26 CN CN201480032446.0A patent/CN105264292B/en active Active
- 2014-05-26 WO PCT/EP2014/060811 patent/WO2014195168A1/en active Application Filing
- 2014-05-26 BR BR112015030027-8A patent/BR112015030027B1/en active IP Right Grant
- 2014-05-26 UA UAA201512876A patent/UA119040C2/en unknown
-
2015
- 2015-10-15 IL IL242086A patent/IL242086B/en active IP Right Grant
- 2015-11-12 US US14/939,567 patent/US10082289B2/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5562437A (en) * | 1993-06-22 | 1996-10-08 | Enterprise Generale De Chauffage Industriel Pillard (Societe Anonyme) | Liquid or gaseous fuel burner with very low emission of nitrogen oxides |
| DE19850940A1 (en) * | 1998-11-05 | 2000-05-31 | Messer Austria Gmbh Gumpoldski | Swirl burner |
| EP1783426A1 (en) * | 2005-11-07 | 2007-05-09 | Riello S.p.A. | Combustion head for a gas burner |
| CN101956974A (en) * | 2009-07-16 | 2011-01-26 | 毛羽 | Novel high-efficiency and low-NOx gas burner capable of controlling flame profile |
| CN202277828U (en) * | 2010-02-18 | 2012-06-20 | 赫多特普索化工设备公司 | Combustor |
Also Published As
| Publication number | Publication date |
|---|---|
| EA032737B1 (en) | 2019-07-31 |
| CA2910908C (en) | 2020-01-21 |
| UA119040C2 (en) | 2019-04-25 |
| US20160061443A1 (en) | 2016-03-03 |
| MX365759B (en) | 2019-06-13 |
| MY173755A (en) | 2020-02-19 |
| CA2910908A1 (en) | 2014-12-11 |
| EA201600001A1 (en) | 2016-04-29 |
| BR112015030027A2 (en) | 2017-07-25 |
| IL242086B (en) | 2020-05-31 |
| BR112015030027B1 (en) | 2021-08-31 |
| ES2748179T3 (en) | 2020-03-13 |
| MX2015015931A (en) | 2016-04-06 |
| EP2811228A1 (en) | 2014-12-10 |
| EP2811228B1 (en) | 2019-08-07 |
| DK2811228T3 (en) | 2019-11-04 |
| US10082289B2 (en) | 2018-09-25 |
| WO2014195168A1 (en) | 2014-12-11 |
| PL2811228T3 (en) | 2020-01-31 |
| CN105264292A (en) | 2016-01-20 |
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